EP2723676B1 - Procédé de production d'ammoniac et d'urée - Google Patents

Procédé de production d'ammoniac et d'urée Download PDF

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EP2723676B1
EP2723676B1 EP12732728.6A EP12732728A EP2723676B1 EP 2723676 B1 EP2723676 B1 EP 2723676B1 EP 12732728 A EP12732728 A EP 12732728A EP 2723676 B1 EP2723676 B1 EP 2723676B1
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gas
partial oxidation
oxygen
ammonia
hydrogen
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EP2723676A1 (fr
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Gaetano Iaquaniello
Barbara CUCCHIELLA
Elena ANTONETTI
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Stamicarbon BV
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    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/025—Preparation or purification of gas mixtures for ammonia synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
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    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/386—Catalytic partial combustion
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    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C273/00—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups
    • C07C273/02—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds
    • C07C273/04—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds from carbon dioxide and ammonia
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
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    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C01B2203/0288—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step containing two CO-shift steps
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0435—Catalytic purification
    • C01B2203/0445—Selective methanation
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    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
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    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/068—Ammonia synthesis
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1258—Pre-treatment of the feed
    • C01B2203/1264—Catalytic pre-treatment of the feed
    • C01B2203/127—Catalytic desulfurisation
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas

Definitions

  • the invention pertains to a process for the production of ammonia, as well as to a process for producing ammonia and, subsequently, urea.
  • Ammonia is generally produced by reacting hydrogen and nitrogen, according to the following reaction equation: 3H 2 +N 2 ⁇ 2NH 3
  • the H 2 is generally obtained from synthesis gas (normally known as "syngas”), which in turn is obtained from a hydrocarbon feed material, which is subjected to steam reforming so as to produce a mixture comprising carbon monoxide (CO), hydrogen (H 2 ), and carbon dioxide (CO 2 ), usually followed by a water gas shift reaction wherein carbon monoxide reacts with water so as to form carbon dioxide and hydrogen.
  • synthesis gas normally known as "syngas”
  • CO carbon monoxide
  • H 2 hydrogen
  • CO 2 carbon dioxide
  • N 2 nitrogen
  • the latter is either present in the original gas mixture (as it is inert with respect to all steps preceding the ammonia synthesis conditions), or added later if obtained from air, in a unit separating nitrogen from oxygen.
  • the hydrogen and nitrogen are subjected to compression and conversion into ammonia in a synthesis reactor.
  • Ammonia is frequently used as a starting material in the synthesis of urea.
  • Urea (NH 2 CONH 2 ) can be produced from ammonia and carbon dioxide at an elevated temperature of, typically, between 150°C and 250°C and an elevated pressure of, typically, between 12 and 40 MPa, in the synthesis zone of a urea plant. In this synthesis, two consecutive reaction steps can be considered to take place. In the first step ammonium carbamate is formed, and in the next step, this ammonium carbamate is dehydrated so as to give urea: (i) 2NH 3 + CO 2 ⁇ H 2 N - CO - ONH 4 (ii) H 2 N - CO - ONH 4 ⁇ H 2 N - CO - NH 2 + H 2 O
  • a disadvantage of this process is that significant energy is used to separate the air into nitrogen and oxygen but no use is made of the oxygen so produced.
  • WO90/06281 discloses a process for making ammonia. Sulphur is removed from an organic feedstock, which is then subjected to catalytic partial oxidation. The synthesis gas then undergoes a CO-shift, carbon dioxide removal and pressure swing adsorption. Nitrogen is then added and ammonia is produced. Purge gas from the pressure swing adsorption is recycled to the catalytic partial oxidation.
  • the invention presents, in one aspect, a process for the production of ammonia, comprising the steps defined in claim 1.
  • the invention concerns a process for the preparation of urea, comprising a process for the preparation of ammonia as defined above, removing CO 2 from the reaction mixture, and reacting the ammonia with the removed CO 2 , under urea-forming conditions.
  • the invention is based on the judicious insight that the use of catalytic partial oxidation in the formation of synthesis gas, rather than steam reforming, is able to bring about unexpected advantages in both the production of ammonia and the production of urea.
  • the CPO reaction is known to the skilled person. It will generally be carried out in a catalytic partial oxidation reactor, comprising a suitable catalyst bed that serves to catalyze the partial oxidation of hydrocarbon into CO and H 2 . It will be understood that some complete oxidation product (viz. CO 2 ) may also be formed.
  • CPO (also often referred to as SCT-CPO) is known to the skilled person.
  • SCT-CPO refers to Short Contact Time Catalytic Partial Oxidation.
  • the CPO reaction takes place in a reactor under the influence of a catalyst at residence times between 10 -2 to 10 -4 and with typical catalyst surface contact times around 10 -6 s -1 . These contact time correspond to typical space velocities of 100,000 to 250,000 hr -1 preferably 100,000 to 200,000 hr -1 .
  • Catalysts employed for SCT-CPO comprise Ni, Pd, Pt, Rh, or Ru.
  • the reaction takes place at catalyst surface temperatures above 950°C, preferably above 1000°C.
  • a reference to CPO is (a) L. Basini, Catalysis Today 117 (2006) 384-393 .
  • Other references include (b) L. Basini, K. Aasberg-Petersen, A. Guarinoni, M. Oestberg, Catalysis Today (2001) 64, 9-20 "Catalytic Partial Oxidation of Natural Gas at Elevated Pressure and Low Residence Time "; (c) H. Hickman, L.D. Schmidt, J. Catal. 138 (1992) 267 ; (d) D. Hichman, L.D.
  • ammonia requires the availability of nitrogen (N 2 ) as a reactant. Nitrogen is obtained from air, and in regular processes this results in oxygen (O 2 ) being lost.
  • oxygen O 2
  • the combination, according to the invention, of a catalytic partial oxidation step and the synthesis of ammonia presents a highly economical advancement. This presents in fact a synergy, in the sense that the oxygen required for catalytic partial oxidation is available by virtue of the production of ammonia and, put otherwise, oxygen normally lost can now be used.
  • the process of the invention starts with the catalytic partial oxidation of a hydrocarbon material.
  • the hydrocarbon material can be a single hydrocarbon, a mixture of hydrocarbons, or any other composition comprising at least one hydrocarbon.
  • Preferred sources are natural gas (CH 4 ), liquid hydrocarbons (such as naphta), gasification of coal, biomass, and waste-to-energy gasification facilities. As conventional, in the event that natural gas is employed, this will generally be desulphurized before being subjected to the process of the invention.
  • the hydrocarbon material can be in a gaseous (e.g. methane or natural gas) and/or in a liquid state and also from biomass.
  • the hydrocarbon material may be suitable for direct feed to the CPO or can be pre-treated for removal of any impurities, such as sulphur compounds, that might be present.
  • the hydrocarbon material is selected from the group consisting of natural gas, Liquefied Petroleum Gas (LPG), refinery gas, naphtha, and mixtures thereof.
  • LPG Liquefied Petroleum Gas
  • refinery gas refinery gas
  • naphtha and mixtures thereof.
  • a CPO reactor generally comprises a reaction zone, made up of a vertical cylindrically shaped steel pressure vessel lined with a refractory material.
  • a CPO reactor typically is distinguished from an autothermal reformer reactors, as the latter comprises a burner, which a CPO generally does not.
  • a mixer such as shown in WO2007045457 may be used to introduce feed streams into the reactor.
  • the CPO process results in synthesis gas, or syngas, comprising CO, CO 2 and H 2 .
  • synthesis gas or syngas
  • methane as an exemplary hydrocarbon feed material
  • the reaction equation for the CPO process is: CH 4 +0.5 O 2 ⁇ CO+2H 2
  • the CPO reaction is known to the skilled person. It will generally be carried out in a catalytic partial oxidation reactor, comprising a suitable catalyst bed that serves to catalyze the partial oxidation of hydrocarbon into CO and H 2 . It will be understood that some complete oxidation product (viz. CO 2 ) may also be formed.
  • CPO (also often referred to as SCT-CPO) is known to the skilled person.
  • SCT-CPO refers to Short Contact Time Catalytic Partial Oxidation.
  • the CPO reaction takes place in a reactor under the influence of a catalyst at residence times between 10 -2 to 10 -4 and with typical catalyst surface contact times around 10 -6 s -1 . These contact time correspond to typical space velocities of 100,000 to 250,000 hr -1 preferably 100,000 to 200,000 hr -1 .
  • Catalysts employed for SCT-CPO comprise Ni, Pd, Pt, Rh, or Ru.
  • the reaction takes place at catalyst surface temperatures above 950°C, preferably above 1000°C.
  • a reference to CPO is (a) L. Basini, Catalysis Today 117 (2006) 384-393 .
  • Other references include (b) L. Basini, K. Aasberg-Petersen, A. Guarinoni, M. Oestberg, Catalysis Today (2001) 64, 9-20 "Catalytic Partial Oxidation of Natural Gas at Elevated Pressure and Low Residence Time "; (c) H. Hickman, L.D. Schmidt, J. Catal. 138 (1992) 267 ; (d) D. Hichman, L.D.
  • oxygen is to be provided in order to effect the oxidation.
  • the oxygen can be in the form of air, a drawback thereof is that this means that a relatively large amount of nitrogen, which is inert until the ammonia-forming reaction, will have to be carried through the process.
  • This requires a much larger equipment than would be strictly necessary for the reactions to be conducted, which is economically undesirable, and is associated with other drawbacks such as a need for building a facility occupying an unduly large ground surface area
  • the catalytic partial oxidation is conducted under the influence of an oxygen-containing gas-stream comprising at least 40% oxygen, preferably at least 60% oxygen. More preferably, the oxygen-containing gas-stream is oxygen having a purity of from 90%-100%.
  • a further advantage of using catalytic partial oxidation is that a synthesis gas can be produced having the proper H 2 /CO 2 ratio to maximize the yield of ammonia and urea in relation to the feed composition.
  • S/C steam to carbon
  • O 2 /C oxygen to carbon
  • the amount of CO 2 produced in the synthesis gas is sufficiently high to use all of the produced NH 3 , without any external support or excess of NH 3 .
  • the skilled person is aware, without undue experimentation, how to calculate the proper amounts of reactants needed in the synthesis gas, and how to set the catalytic partial oxidation process so as to achieve this.
  • the CPO reactor is operated with a steam to carbon ratio (S/C) in the range of 0,3-1,0, preferably in the range of 0.4 to 0.6.
  • the oxygen to carbon ratio (O/C) is in the range of 0.3-0.7, preferably in the range of 0.5-0.7.
  • the raw gas obtained from the catalytic partial oxidation has a temperature between about 900°C and 1200°C, preferably between 950-1050 °C, better around 1000 °C.
  • the mixture is subjected to a water gas shift reaction.
  • WGSR water gas shift reactor
  • the synthesis gas is generally cooled down, either in a process gas boiler or in a direct quencher, before entering the WGS reactor, producing a shifted synthesis gas stream.
  • this subsequent step of converting CO into CO 2 by means of a water gas shift reactor is represented by the following reaction equation: CO+ 2H 2 + H 2 O ⁇ CO 2 + 3H 2
  • the WGS reaction is typically carried out using either a single stage or multi stage to attain the desired degree and rate of conversion.
  • the high temperature stage operates at 300-450°C and typically in the presence of an iron-based catalyst such as Fe/Cr.
  • the largest amount of CO is converted, usually more than 90% such as between 96 and 98%.
  • the following stage can be a high, medium or low temperature stage (HTS, MTS or LTS); using MTS or LTS, the operating temperature is about 180-280°C and typically a copper/zinc catalyst supported on alumina (Cu/Zn/Al) catalyst is used. In these latter stages the residual CO concentration in the outlet stream is typically as low as 0.1-0.3%.
  • the gas stream resulting from the WGSR contains mainly hydrogen and carbon dioxide.
  • hydrogen is separated from this stream by pressure swing absorption (PSA) to yield a pure hydrogen stream and a purge gas stream (which typically comprises H 2 , CH 4 , CO, and CO 2 ).
  • PSA pressure swing absorption
  • the purge gas from PSA is recycled to the CPO reactor in order to have a 100% conversion of the feed.
  • the process of the invention is used for the production of ammonia.
  • This requires providing hydrogen as a reactant, in accordance with the aforementioned step (d), viz. separating hydrogen from the reaction mixture.
  • the separation of hydrogen from the reaction mixture resulting from the water gas shift reaction by removing CO 2 from the gas mixture comprising hydrogen and carbon dioxide, so as to obtain a gas mixture enriched in H 2 .
  • the latter is reacted with N 2 so as to form ammonia.
  • This reaction is well-known, and the skilled person is familiar with production methods and plants to carry this out.
  • the oxygen used in the catalytic partial oxidation and the nitrogen used in the ammonia-forming reaction are obtained from an air separation unit.
  • the invention pertains to a process for the production of ammonia, comprising the steps of
  • the catalytic partial oxidation should preferably be understood as it is understood in the art, viz. as being of the above-explained short contact time (SCT) type.
  • SCT short contact time
  • nitrogen and oxygen are produced generally acccording to the following equation: 1,88 N 2 + 0.5 O 2 (air) ⁇ 1,88 N 2 + 0.5 O 2
  • Air separation units are known to the skilled person. Air separation units employing cryogenic, adsorption air separation, vacuum swing adsorption or membrane air separation may be used. In a preferred embodiment a cryogenic air separation process is used as it can yield highly pure nitrogen and oxygen. In the process large volumes of air from the atmosphere are compressed, cooled and liquefied. After compression impurities are removed and the nitrogen and oxygen are separated by distillation. A comprehensive overview may be found in the Nexant PERP 08/09S1 (February 2010) report. It will be understood that the oxygen and the nitrogen can also be produced in different air separation units. Preferably, the nitrogen and the oxygen used in the process come from the same air separation unit.
  • the process of the invention is used for the production of urea.
  • the ammonia is then reacted with the removed CO 2 under urea-forming conditions. This reaction too is well-known, and production methods and plants are available to the skilled person.
  • Urea (NH 2 CONH 2 ) can be produced from ammonia and carbon dioxide at an elevated temperature (typically, between 150°C and 250°C) and elevated pressure (typically between 12 and 40 MPa) in the synthesis zone of a urea plant. In this synthesis, two consecutive reaction steps can be considered to take place.
  • ammonium carbamate is formed, and in the next step, this ammonium carbamate is dehydrated so as to give urea
  • the first step (i) is exothermic, and the second step can be represented as an endothermic equilibrium reaction (ii): (i) 2NH 3 + CO 2 ⁇ H 2 N - CO - ONH 4 (ii) H 2 N - CO - ONH 4 ⁇ H 2 N - CO - NH 2 + H 2 O
  • a typical urea production plant the foregoing reactions are conducted in a urea synthesis section so as to result in an aqueous solution comprising urea.
  • this solution is concentrated to eventually yield urea in a form of a melt rather than a solution.
  • This melt is further subjected to one or more finishing steps, such as prilling, granulation, pelletizing or compacting.
  • the invention provides a very economical way of using the components of the gas mixture obtained, in producing the important bulk chemical compound, urea.
  • the excess of nitrogen from the air separation unit may be used within the production facilities or sold to other users.
  • Fig. 1 a typical representation is given of an embodiment known in the art.
  • a feed gas stream enters a desulphurisation unit.
  • the resulting stream is mixed with steam and fed to the steam reforming reactor (SR).
  • the syngas at the outlet of SR is cooled down and then introduced into a water gas shift section.
  • the resulting shifted gas is cooled down and purified into a Pressure Swing Absorption (PSA) unit producing an ultra pure hydrogen stream and a purge gas which is burnt in the SR furnace.
  • PSA Pressure Swing Absorption
  • Nitrogen is obtained from the Air Separtion Unit (ASU) where also an oxygen stream is produced.
  • ASU Air Separtion Unit
  • FIG 2 one embodiment of the present invention is presented.
  • a feed gas stream 101 enters a desulphurisation unit 10 after mixing with stream 103, the purge gas from PSA. It is remarked that stream 103 is not correctly as shown in the figure, and should flow to upstream of unit 10 where it is mixed with stream 101.
  • the resulting stream is mixed in a proper device, 20, with another stream containing oxygen and steam (resulting from mixing stream 102 and steam) before being fed to the CPO reactor as feed stream to unit 30.
  • a pre-reformer (not shown) is upstream of CPO reactor 30.
  • the CPO reactor 30 may be a steel vessel internally lined for converting hydrocarbons, such as natural gas , LPG, refinery gas, naphta and even heavier feed.
  • the CPO reactor preferably operates with a steam to carbon ratio (S/C) in the range of 0.3-1.0, preferably in the range of 0.4 to 0.6.
  • the oxygen to carbon ratio (O 2 /C) preferably is in the range of 0.4-0.7 more preferably in the range of 0.5-0.7.
  • the syngas at the outlet of the CPO reactor preferably is in the temperature range of 800°C-1200°C, more preferably between 900°C and 1050°C.
  • the syngas stream 105 is cooled by indirect heat exchange raising steam 106 in a process gas boiler 40 (in an alternative embodiment it may be cooled by a direct water quenching).
  • the quenched syngas 107 is then introduced into a CO shift reactor 50.
  • the shift reactor 50 may be in one stage or two stages with an intercooler (in a alternative embodiment it may be an isothermal shift convertor).
  • Shift reactor 50 typically uses, e.g., an iron based catalyst and/or a copper based catalyst.
  • the resulting shifted gas 108 is cooled down and introduced into a CO 2 removal unit 60 where all of the CO 2 goes into a stream 109.
  • the CO 2 removal unit 60 may be a solvent wash system, such as amine, selexol or other know solvents, or by other means known to the skilled person.
  • the amount of CO 2 may be varied but for a ammonia /urea production plant, it will be as high as possible.
  • the raw hydrogen gas is then purified in a pressure Swing Absorption (PSA) unit 70 producing an ultra pure hydrogen stream 111 and a purge gas 103 which after compression is recycled to the CPO reactor 30, A complete recycle of the purge gas will yield almost 100% conversion of the carbon fraction of the feed to CO 2 and 100% of H 2 recovery and use.
  • PSA pressure Swing Absorption
  • the present invention enables recovering almost 100% of the total carbon dioxide generation from high pressure syngas as opposed to the 50-60% of a more conventional steam reforming (SR) technology.
  • SR steam reforming
  • Pure hydrogen 111 is mixed with a nitrogen stream in a ratio of about 3:1 before being compressed and introduced into the ammonia synthesis reactor.
  • Nitrogen is obtained from the Air Separtion Unit (ASU) 90 where also the oxygen stream 102 is produced.
  • streams 112 and 102 are produced in different ASUs.
  • any process for ammonia synthesis may be used. The most common industial process for ammonia synthesis involving forming a mixture of gaseous nitrogen and hydrogen in a 1 to 3 ratio, plus minor components as CH 4 and CO 2 .
  • the present invention allows to feed to the synthesis reactor pure components and minimizing any purge. This results in improved energy efficiency of the overall manufacturing process.
  • the mixture compressed at higher pressure e.g. in the range of 80-200 barg, reacts in accordance with the following reaction : 3H 2 + N 2 ⁇ 2NH 3
  • ammonia is then combined with the CO 2 removed from the syngas and sent to a urea production unit, 95.
  • a urea production unit 95.
  • any process for urea synthesis may be used .

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Claims (9)

  1. Procédé pour la production d'ammoniaque, comprenant les étapes de
    (a) fourniture d'un matériau hydrocarboné ;
    (b) soumission du matériau hydrocarboné à une oxydation partielle catalytique (CPO) afin de produire un gaz de synthèse comprenant du monoxyde de carbone, de l'hydrogène et du dioxyde de carbone ;
    (c) soumission du gaz de synthèse à une réaction de conversion à la vapeur d'eau afin de faire réagir le monoxyde de carbone avec de l'eau avec la formation d'un mélange gazeux comprenant de l'hydrogène et du dioxyde de carbone ;
    (d) séparation d'hydrogène du mélange réactionnel ;
    (e) réaction de l'hydrogène avec de l'azote dans des conditions de formation d'ammoniaque afin de produire de l'ammoniaque, dans lequel l'oxydation partielle catalytique est une oxydation partielle catalytique à courte durée de contact, réalisée à une vitesse spatiale de 100 000 à 250 000 hr-1, dans lequel l'oxygène utilisé dans l'oxydation partielle catalytique et l'azote utilisé dans la réaction de formation d'ammoniaque sont obtenus à partir d'une unité de séparation d'air,
    dans lequel l'hydrogène est séparé du mélange réactionnel en éliminant CO2 du mélange gazeux comprenant de l'hydrogène et du dioxyde de carbone, afin d'obtenir un mélange de gaz enrichi en H2,
    dans lequel l'hydrogène est purifié en utilisant un Pressure Swing Absorber (absorbeur à modulation de pression) après l'élimination de CO2, pour produire un courant d'hydrogène pur et un courant de gaz de purge, lequel gaz de purge est recyclé dans le réacteur CPO avec un recyclage complet du gaz de purge,
    dans lequel le rapport oxygène à carbone dans l'oxydation partielle catalytique est de 0,3 à 0,7, et dans lequel le rapport vapeur à carbone dans l'oxydation partielle catalytique se trouve dans l'intervalle de 0,3 - 1,0.
  2. Procédé selon la revendication 1, dans lequel la vitesse spatiale est de 100 000 à 200 000 hr-1.
  3. Procédé selon l'une quelconque des revendications précédentes, dans lequel l'oxydation partielle catalytique est réalisée sous l'influence d'un courant de gaz contenant de l'oxygène comprenant au moins 40 % d'oxygène, de préférence au moins 60 % d'oxygène.
  4. Procédé selon l'une quelconque des revendications précédentes, dans lequel le courant de gaz contenant de l'oxygène est de l'oxygène ayant une pureté de 90 %-100 %.
  5. Procédé selon la revendication 1, comprenant une purification supplémentaire de H2 par méthanation de CO et CO2.
  6. Procédé pour la préparation d'urée, comprenant un procédé pour la production d'ammoniaque selon l'une quelconque des revendications 1 à 5, et la réaction de l'ammoniaque avec le CO2 éliminé, dans des conditions de formation d'urée.
  7. Procédé selon l'une quelconque des revendications précédentes, dans lequel le matériau hydrocarboné est choisi dans le groupe consistant en gaz naturel, gaz de pétrole liquéfié (LPG), gaz de raffinerie, naphtha, et mélanges de ceux-ci.
  8. Procédé selon l'une quelconque des revendications précédentes, dans lequel le rapport oxygène à carbone (O/C) dans l'oxydation partielle catalytique est de 0,5 à 0,7, et dans lequel le rapport vapeur à carbone (S/C) dans l'oxydation partielle catalytique se trouve dans l'intervalle de 0,4 - 0,6.
  9. Procédé selon l'une quelconque des revendications précédentes, dans lequel le gaz brut obtenu à partir de l'oxydation partielle catalytique présente une température d'environ 900°C à 1 200°C.
EP12732728.6A 2011-06-23 2012-06-25 Procédé de production d'ammoniac et d'urée Active EP2723676B1 (fr)

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EP11171166 2011-06-23
PCT/NL2012/050444 WO2012177137A1 (fr) 2011-06-23 2012-06-25 Procédé de production d'ammoniac et d'urée
EP12732728.6A EP2723676B1 (fr) 2011-06-23 2012-06-25 Procédé de production d'ammoniac et d'urée

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EP2867484B1 (fr) 2012-06-27 2020-02-12 Grannus, LLC Production par génération multiple d'énergie et d'engrais au moyen d'une capture d'émissions
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US10106430B2 (en) 2013-12-30 2018-10-23 Saudi Arabian Oil Company Oxycombustion systems and methods with thermally integrated ammonia synthesis
US10196348B2 (en) * 2014-07-15 2019-02-05 Stamicarbon B.V. Method for revamping a urea production complex
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US20140170052A1 (en) 2014-06-19
CA2835472C (fr) 2018-07-31
EP2723676A1 (fr) 2014-04-30
WO2012177137A1 (fr) 2012-12-27
CA2835472A1 (fr) 2012-12-27
DK2723676T3 (en) 2019-02-25
US9598290B2 (en) 2017-03-21
LT2723676T (lt) 2019-03-12
CN103648970A (zh) 2014-03-19

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